JP3742916B2

JP3742916B2 - Air-cooled absorption refrigeration system

Info

Publication number: JP3742916B2
Application number: JP11110897A
Authority: JP
Inventors: 則之奥田; 晃一安尾; 史朗薬師寺; 正人内海
Original assignee: Daikin Industries Ltd
Current assignee: Daikin Industries Ltd
Priority date: 1997-04-28
Filing date: 1997-04-28
Publication date: 2006-02-08
Anticipated expiration: 2017-04-28
Also published as: JPH10300262A

Description

【０００１】
【発明の属する技術分野】
【０００２】
本願発明は、空冷吸収式冷凍装置に関し、さらに詳しくは空冷吸収式冷凍装置における２次冷媒の過熱を防止する機構に関するものである。
【従来の技術】
【０００３】
一般に、空冷吸収式冷凍装置は、１次冷媒が循環し、再生器、気液分離器、１次冷媒（例えば、１次冷媒蒸気）から暖房熱源を得る温熱熱交換器、空冷凝縮器、１次冷媒（例えば、凝縮１次冷媒液）から冷房熱源を得る蒸発器および空冷吸収器を接続してなる１次冷媒回路と、２次冷媒が循環し、前記温熱熱交換器、利用側熱交換器および前記蒸発器を接続してなる２次冷媒回路とを備えて構成されている。
【発明が解決しようとする課題】
【０００４】
上記のような構成の空冷吸収式冷凍装置の場合、暖房運転時における暖房熱源として気液分離器から供給される高温の１次冷媒蒸気の保有する熱を温熱熱交換器により２次冷媒へ伝達するようにしているため、冷房運転時においても、温熱熱交換器を流れる２次冷媒は、高温の１次冷媒蒸気にさらされることとなる。この場合、２次冷媒として水を用いている空冷吸収式冷凍装置においては、２次冷媒回路を循環する水が高圧となるおそれがある点を除いてあまり問題はない。なお、循環水の高圧化を防止するために、冷水が得られる蒸発器と温熱熱交換器とを直列に接続したものがある。
【０００５】
ところが、２次冷媒としてフロン系冷媒（例えば、Ｒ４０７ｃ等の混合冷媒）を用いた場合、空冷吸収式冷凍装置を上記構成のままとすると、冷房運転時において温熱熱交換器に高温の１次冷媒蒸気（１５０℃以上）が供給されることとなるため、２次冷媒であるフロン系冷媒が高温にさらされることとなる。すると、フロン系冷媒が分解してしまうという不具合が生じる。
【０００６】
本願発明は、上記の点に鑑みてなされたもので、冷房運転時における２次冷媒の異常過熱を防止することにより、２次冷媒にフロン系冷媒を用いたとしても冷媒分解が生じないようにすることを目的とするものである。
【課題を解決するための手段】
【０００７】
本願発明の第１の基本構成では、上記課題を解決するための手段として、１次冷媒が循環し、高温再生器１、気液分離器４、暖房熱源を得るための温熱熱交換器５、低温再生器６、空冷凝縮器９、冷房熱源を得るための蒸発器１２および空冷吸収器１５を順次接続してなる１次冷媒回路Ｘと、２次冷媒ｙが循環し、前記温熱熱交換器５、利用側熱交換器１７および前記蒸発器１２を順次接続してなる２次冷媒回路Ｙとを備えた空冷吸収式冷凍装置において、前記２次冷媒ｙとしてフロン系冷媒を採用するとともに、前記低温再生器６における１次冷媒出口と前記気液分離器４との間に、前記温熱熱交換器５を介設し且つ該温熱熱交換器５とを連通する凝縮液還流回路２１に、冷房運転時に閉弁し、暖房運転時に開弁する開閉弁２５を介設している。
【０００８】
上記のように構成したことにより、冷房運転時においては、低温再生器６を通過して飽和した蒸気（１００℃程度）が温熱熱交換器５に流入するため、温熱熱交換器５の温度が１００℃程度に抑えられることとなる。従って、温熱熱交換器５における２次冷媒ｙの異常過熱が防止され、２次冷媒ｙとして用いられているフロン系冷媒の分解が防止されることとなり、装置の信頼性を確保することができる。また、暖房運転時においては、気液分離器４から低温再生器６を経て温熱熱交換器５へ１次冷媒蒸気ａ（１３０℃程度）が供給されることとなり、該１次冷媒蒸気ａの保有する熱が暖房熱源として２次冷媒ｙへ伝達されることとなる。従って、暖房運転時における成績係数（ＣＯＰ）の低下を防止することができる。
【０００９】
本願発明の第１の基本構成において、前記凝縮液還流回路２１に、前記開閉弁２５に代えて液シール部３０を設けた場合、開閉弁２５を省略できることとなり、コストダウンに寄与する。
【００１０】
本願発明の第２の基本構成では、上記課題を解決するための手段として、１次冷媒が循環し、高温再生器１、気液分離器４、暖房熱源を得るための温熱熱交換器５、低温再生器６、空冷凝縮器９、冷房熱源を得るための蒸発器１２および空冷吸収器１５を順次接続してなる１次冷媒回路Ｘと、２次冷媒ｙが循環し、前記温熱熱交換器５、利用側熱交換器１７および前記蒸発器１２を順次接続してなる２次冷媒回路Ｙとを備えた空冷吸収式冷凍装置において、前記２次冷媒ｙとしてフロン系冷媒を採用するとともに、前記低温再生器６における吸収液通路６ａに、前記２次冷媒ｙが供給される温熱熱交換器５の熱交換部を配設している。
【００１１】
上記のように構成したことにより、冷房運転時においては、低温再生器６における吸収液温度は飽和蒸気（１００℃程度）と同等となっているため、温熱熱交換器５の温度が１００℃程度に抑えられることとなる。従って、温熱熱交換器５における２次冷媒ｙの異常過熱が防止され、２次冷媒ｙとして用いられているフロン系冷媒の分解が防止されることとなり、装置の信頼性を確保することができる。また、暖房運転時においては、気液分離器４から低温再生器６に供給される吸収液（１３０℃程度）の保有する熱が暖房熱源として２次冷媒ｙへ伝達されることとなる。従って、暖房運転時における成績係数（ＣＯＰ）の低下を防止することができる。
【００１２】
本願発明の第２の基本構成において、前記気液分離器４から前記低温再生器６へ供給される中間濃溶液と前記空冷吸収器１５から前記気液分離器４へ還流される吸収希溶液とを熱交換させる高温溶液熱交換器７と、前記中間濃溶液が流通する配管に、前記高温溶液熱交換器７をバイパスし且つ暖房運転時にのみ開通するバイパス回路３２とを設けた場合、暖房運転時において低温再生器６へは高温溶液熱交換器７をバイパスした（即ち、高温溶液熱交換器７において吸収希溶液ｃに熱回収されない）中間濃溶液ｂが供給されることとなり、冷房運転時において高温再生器１へ還流される吸収希溶液ｃへの熱回収を有効に行いつつ、暖房運転時における成績係数（ＣＯＰ）の低下を防止することができる。
【００１３】
本願発明の第３の基本構成では、上記課題を解決するための手段として、１次冷媒が循環し、高温再生器１、気液分離器４、暖房熱源を得るための温熱熱交換器５、低温再生器６、空冷凝縮器９、冷房熱源を得るための蒸発器１２および空冷吸収器１５を順次接続してなる１次冷媒回路Ｘと、２次冷媒ｙが循環し、前記温熱熱交換器５、利用側熱交換器１７および前記蒸発器１２を順次接続してなる２次冷媒回路Ｙとを備えた空冷吸収式冷凍装置において、前記２次冷媒ｙとしてフロン系冷媒を採用するとともに、前記気液分離器４から前記低温再生器６へ供給される中間濃溶液ｂと前記空冷吸収器１５から前記気液分離器４へ還流される吸収希溶液ｃとを熱交換させる高温溶液熱交換器７を付設し且つ該高温溶液熱交換器７の下流側に前記温熱熱交換器５を配設する一方、前記温熱熱交換器５における１次冷媒通路の出口を、前記気液分離器４からの１次冷媒蒸気ａが供給されるとともに前記温熱熱交換器５より高位であって前記気液分離器４と同一高さもしくはそれより低位に配置された暖房用吸収器５３を介して前記高温再生器１に接続している。
【００１４】
上記のように構成したことにより、冷房運転時においては、高温溶液熱交換器７の下流側の吸収液温度は高温溶液熱交換器７における熱回収により１３０℃程度となっているため、温熱熱交換器５の温度が１３０℃程度に抑えられることとなる。従って、温熱熱交換器５における２次冷媒ｙの異常過熱が防止され、２次冷媒ｙとして用いられているフロン系冷媒の分解が防止されることとなり、装置の信頼性を確保することができる。また、暖房運転時においては、気液分離器４から高温溶液熱交換器７を通過した中間濃溶液ｂ（１３０℃程度）の保有する熱が暖房熱源として２次冷媒ｙへ伝達されることとなる。従って、暖房運転時における成績係数（ＣＯＰ）の低下を防止することができる。しかも、暖房運転時において温熱熱交換器５の１次冷媒通路に供給された吸収濃溶液ｂが暖房吸収器５３に入り、そこで１次冷媒蒸気ａを吸収して吸収希溶液ｃとなって高温再生器１へ還流されるようにしているので、暖房運転時における１次冷媒の搬送をスムーズに行うことができる。
【００１５】
本願発明の第３の基本構成において、前記温熱熱交換器５と前記高温溶液熱交換器７とを一体化した場合、コストダウンを図ることができる。
【発明の実施の形態】
【００１６】
以下、添付の図面を参照して、本願発明の幾つかの好適な実施の形態および参考例について詳述する。
【００１７】
以下の各実施の形態および参考例においては、吸収液として例えば臭化リチウム水溶液（ＬｉＢｒ水溶液）が採用され、１次冷媒回路Ｘを循環する１次冷媒として水および水蒸気が採用され、２次冷媒回路Ｙを循環する２次冷媒ｙとしてフロン系冷媒（例えば、Ｒ４０７ｃ等の混合冷媒）が採用されている。
【００１８】
第１の実施の形態（請求項１に対応）
図１には、本願発明の第１の実施の形態にかかる空冷吸収式冷凍装置の全体的な冷凍システムの構成が示されている。
【００１９】
図１において、符号１は高温再生器であり、ガスバーナ等の加熱源２を備えている。該高温再生器１の上方には、沸騰気液通路３を介して連通された気液分離器４が設けられている。前記高温再生器１においては、吸収希溶液ｃ（即ち、臭化リチウム希溶液）を加熱沸騰させて、沸騰気液通路３を介して上方に位置する気液分離器４に供給し、ここで１次冷媒蒸気である水蒸気ａと吸収濃溶液ｂ（即ち、臭化リチウム濃溶液）とに分離再生するようになっている。
【００２０】
前記臭化リチウム希溶液ｃは、後に詳述する空冷吸収器１５において吸収濃溶液である臭化リチウム濃溶液ｂに１次冷媒凝縮液である水ｄを吸収して得られ、低温溶液熱交換器１４および高温溶液熱交換器７を経て予熱されて気液分離器４に供給され、その後高温再生器１へ還流されることとなっている。
【００２１】
前記気液分離器４において分離された水蒸気ａは低温再生器６に送られる。一方、前記気液分離器４において分離された臭化リチウムの中間濃溶液ｂは、前記高温溶液熱交換器７において前記した臭化リチウム希溶液ｃと熱交換した後に前記低温再生器６の吸収液通路６ａへ供給される。なお、低温再生器６に供給される中間濃溶液ｂの温度は１３０℃程度とされる。符号８は排ガスを排出するための排ガス通路である。
【００２２】
前記低温再生器６においては、気液分離器４から供給された水蒸気ａと中間濃溶液ｂとを熱交換させることにより、水蒸気ａを凝縮させるとともに中間濃溶液ｂ中に含まれる残余水分を蒸発させてさらに高濃度の臭化リチウム溶液をとりだす。
【００２３】
前記低温再生器６において中間濃溶液ｂから蒸発された水蒸気ａは、空冷凝縮器９に送られて凝縮液化されて１次冷媒凝縮液（即ち、凝縮水ｄ）となり冷媒タンク１０に溜められる。また、前記低温再生器６において凝縮液化された凝縮水ｄも空冷凝縮器９の下端において合流した後冷媒タンク１０に溜められる。なお、低温再生器６を出た水蒸気ａは飽和蒸気（１００℃程度）となっている。
【００２４】
前記冷媒タンク１０に溜められた凝縮水ｄは、冷媒ポンプ１１により蒸発器１２の散布装置１３へ供給される。また、前記低温再生器６から取り出された臭化リチウム濃溶液ｂは、低温溶液熱交換器１４において前記した臭化リチウム希溶液ｃと熱交換した後に空冷吸収器１５の吸収液分配容器１６に供給される。
【００２５】
前記蒸発器１２は、利用側熱交換器１７を含む２次冷媒回路Ｙを循環する２次冷媒ｙ（例えば、Ｒ４０７Ｃ等）と冷媒タンク１０から送られる凝縮水ｄとを熱交換させるものであり、冷房運転時の冷熱源を得る作用をなす。なお、蒸発器１２において蒸発しきれなかった凝縮水ｄは、凝縮水還流回路２９を介して冷媒ポンプ１１の上流側に還流される。
【００２６】
そして、前記空冷吸収器１５から取り出された臭化リチウム希溶液ｃは、溶液ポンプ１８により前述したように低温溶液熱交換器１４および高温溶液熱交換器７を経て気液分離器４に戻される。
【００２７】
しかして、本実施の形態においては、低温再生器６における１次冷媒出口（換言すれば、蒸気出口６ｂ）と前記気液分離器４との間には、暖房熱源を得るための温熱熱交換器５が介設されており、該温熱熱交換器５と該気液分離器４とを連通する凝縮液還流回路２１に、冷房運転時に閉弁し、暖房運転時に開弁する開閉弁２５が介設されている。この温熱熱交換器５は、後に詳述する利用側熱交換器１７を含む２次冷媒回路Ｙを循環する２次冷媒ｙ（例えば、Ｒ４０７ｃ）と低温再生器６を通過した飽和水蒸気（１００℃程度）とが熱交換して暖房運転時の温熱源を得る作用をなす。そして、温熱熱交換器５において凝縮した１次冷媒凝縮液ｄ（即ち、凝縮水）は凝縮液還流回路２１を介して前記気液分離器４へ還流される。なお、低温再生器６の蒸気出口６ｂから温熱熱交換器５に至る配管に、冷房運転時に閉弁され、暖房運転時に開弁される開閉弁を介設してもよい。この温熱熱交換器５としては、シェルアンドコイル式熱交換器、シェルアンドチューブ式熱交換器、二重管式熱交換器、プレート式熱交換器等が採用される。
【００２８】
図面中、符号２６，２７は冷暖切換弁であり、それぞれ冷房運転時には開弁され、暖房運転時には閉弁されることとなっている。
【００２９】
上記のように構成された空冷吸収式冷凍装置は、次のように作用する。
（Ｉ）冷房運転時
開閉弁２５を閉弁し、冷暖切換弁２６，２７を開弁した状態において、加熱源であるガスバーナ２に点火して高温再生器１を作動させると、沸騰気液が気液分離器４へ供給され、ここで水蒸気ａと臭化リチウムの中間濃溶液ｂとに分離され、水蒸気ａは低温再生器６へ、中間濃溶液ｂは高温溶液熱交換器７において臭化リチウム希溶液ｃを加熱した後低温再生器６へ供給される。
【００３０】
低温再生器６においては、中間濃溶液ｂが水蒸気ａとの熱交換により加熱されて水蒸気ａを蒸発させ、自身さらに濃縮される。ここで、中間濃溶液ｂとの熱交換により凝縮した凝縮水ｄは空冷凝縮器９の下部を経て冷媒タンク１０に溜め込まれる。一方、低温再生器６において中間濃溶液ｂから蒸発した水蒸気ａは空冷凝縮器９において凝縮されて凝縮水ｄとなり、冷媒タンク１０に溜め込まれる。
【００３１】
冷媒タンク１０に溜められた凝縮水ｄは、冷媒ポンプ１１により散布装置１３へ供給された後、蒸発器１２に散布され、ここで、２次冷媒ｙと熱交換して自身蒸発するとともに、２次冷媒ｙを冷却する。かくして冷却された２次冷媒ｙは利用側熱交換器１７において冷房用の冷熱源として利用される。
【００３２】
一方、前記低温再生器６から取り出された臭化リチウム濃溶液ｂは、低温溶液熱交換器１４において前記した臭化リチウム希溶液ｃと熱交換した後に吸収液分配容器１６を経て空冷吸収器１５に供給され、前記蒸発器１２で得られた水蒸気ａを吸収し、臭化リチウム希溶液ｃとなる。
【００３３】
そして、前記空冷吸収器１５から取り出された臭化リチウム希溶液ｃは、溶液ポンプ１８により前述したように低温溶液熱交換器１４および高温溶液熱交換器７を経る過程において余熱されて気液分離器４に戻される。
【００３４】
上記したように、冷房運転時においては、低温再生器６を通過して飽和した水蒸気ａ（１００℃程度）が温熱熱交換器５に流入するため、温熱熱交換器５の温度が１００℃程度に抑えられることとなる。従って、温熱熱交換器５における２次冷媒ｙの異常過熱が防止され、２次冷媒ｙとして用いられているフロン系冷媒の分解が防止されることとなり、装置の信頼性を確保することができる。
（ＩＩ）暖房運転時
開閉弁２５を開弁し、冷暖切換弁２６，２７を閉弁した状態において、加熱源であるガスバーナ２に点火して高温再生器１を作動させると、沸騰気液が気液分離器４へ供給され、ここで水蒸気ａと臭化リチウムの中間濃溶液ｂとに分離され、水蒸気ａは低温再生器６を経て温熱熱交換器５へ供給される。
【００３５】
そして、温熱熱交換器５においては、２次冷媒ｙとの熱交換により飽和水蒸気ａが凝縮され、得られた凝縮水は凝縮液循環回路２１を介して気液分離器４へ還流され、その後高温再生器１へ戻される。つまり、飽和水蒸気ａの保有する熱は、２次冷媒ｙに暖房用の温熱源として与えられるのである。
【００３６】
上記したように、暖房運転時においては、温熱熱交換器５へ低温再生器６から出た飽和水蒸気ａが供給され、該飽和水蒸気ａの保有する熱が暖房熱源として２次冷媒ｙへ伝達されることとなる。従って、暖房運転時における成績係数（ＣＯＰ）の低下を防止することができる。
【００３７】
第２の実施の形態（請求項２に対応）
図２には、本願発明の第２の実施の形態にかかる空冷吸収式冷凍装置の全体的な冷凍システムの構成が示されている。
【００３８】
この場合、温熱熱交換器５と気液分離器４とを連絡する凝縮液還流回路２１には、開閉弁２５に代えてＵ字管からなる液シール部３０が介設されている。該液シール部３０は、冷房運転時において温熱熱交換器５において凝縮された凝縮水を封入し、低温再生器６から温熱熱交換器５を経て気液分離器４へ飽和水蒸気が短絡してしまうのを防止するものであり、開閉弁と同等の作用をなす。このようにすると、開閉弁が不要となるので、コストダウンに寄与することとなる。その他の構成および作用効果は第１の実施の形態におけると同様なので説明を省略する。
【００３９】
第３の実施の形態（請求項３、４に対応）
図３には、本願発明の第３の実施の形態にかかる空冷吸収式冷凍装置の全体的な冷凍システムの構成が示されている。
【００４０】
この場合、温熱熱交換器５の熱交換部は、低温再生器６における吸収液通路６ａに配設されている。また、冷暖切換弁２６は省略され、中間濃溶液ｂが流通する配管３１には、高温溶液熱交換器７をバイパスし且つ暖房運転時にのみ開通するバイパス回路３２が設けられている。該バイパス回路３２には、冷房運転時に閉弁し、暖房運転時に開弁する開閉弁３３が介設されている。さらに、低温再生器６から低温溶液熱交換器１４に至る配管３４から分岐して高温再生器１に至る分岐回路３５が付設されており、該分岐回路３５には、冷房運転時に閉弁し、暖房運転時に開弁する開閉弁３６が介設されている。符号３７は低温溶液熱交換器１４から吸収液分配容器１６に至る配管に介設された冷暖切換用の開閉弁である。
【００４１】
上記のように構成したことにより、冷房運転時においては、開閉弁３３，３６を閉弁し、冷暖切換弁２７および開閉弁３７を開弁した状態で高温再生器１を駆動させる。すると、低温再生器６の吸収液通路６ａには、気液分離器４により分離された中間濃溶液ｂが高温溶液熱交換器７を経て供給されることとなり、吸収液通路６ａの温度は飽和蒸気（１００℃程度）と同等となる。従って、温熱熱交換器５の温度が１００℃程度に抑えられることとなり、温熱熱交換器５における２次冷媒ｙの異常過熱が防止される結果、２次冷媒ｙとして用いられているフロン系冷媒の分解が防止され、装置の信頼性を確保することができる。
【００４２】
一方、暖房運転時においては、冷暖切換弁２７および開閉弁３７を閉弁し、開閉弁３３，３６を開弁した状態で高温再生器１を駆動させる。すると、低温再生器６の吸収液通路６ａには、気液分離器４により分離された中間濃溶液ｂが直接供給されることとなり、吸収液通路６ａの温度は１３０℃程度となる。従って、暖房運転時においては、気液分離器４から低温再生器６に供給される吸収液（１３０℃程度）の保有する熱が暖房熱源として２次冷媒ｙへ伝達されることとなり、暖房運転時における成績係数（ＣＯＰ）の低下を防止することができる。なお、低温再生器６における２次冷媒ｙとの熱交換により冷却された中間濃溶液ｂは、配管３４および分岐回路３５を介して高温再生器１へ還流される。
【００４３】
その他の構成および作用効果は第１の実施の形態におけると同様なので説明を省略する。
【００４４】
第１の参考例
図４には、第１の参考例にかかる空冷吸収式冷凍装置の全体的な冷凍システムの構成が示されている。
【００４５】
この場合、温熱熱交換器５は、高温溶液熱交換器７の下流側に配設されている。また、この温熱熱交換器５から低温再生器６に至る配管３８における冷暖切換弁２６の上流側から分岐して高温再生器１へ至る分岐回路３９が付設されており、該分岐回路３９には、冷房運転時に閉弁し、暖房運転時に開弁する開閉弁４０が介設されている。
【００４６】
上記のように構成したことにより、冷房運転時においては、開閉弁４０を閉弁し、冷暖切換弁２６，２７を開弁した状態で高温再生器１を駆動させる。すると、温熱熱交換器５には、気液分離器４により分離された中間濃溶液ｂが高温溶液熱交換器７を経て供給されることとなり、温熱熱交換器５の温度が高温溶液熱交換器７における熱回収により１３０℃程度に抑えられることとなる。従って、温熱熱交換器５における２次冷媒ｙの異常過熱が防止されることとなり、２次冷媒ｙとして用いられているフロン系冷媒の分解が防止され、装置の信頼性を確保することができる。
【００４７】
一方、暖房運転時においては、冷暖切換弁２６，２７を閉弁し、開閉弁４０を開弁した状態で高温再生器１を駆動させる。すると、温熱熱交換器５には、気液分離器４により分離された中間濃溶液ｂが高温溶液熱交換器７を経て供給されるが、この時高温溶液熱交換器７には吸収希溶液ｃが供給されていないため、温熱熱交換器５の温度は１３０℃程度となる。従って、暖房運転時においては、気液分離器４から供給される吸収液（１３０℃程度）の保有する熱が暖房熱源として２次冷媒ｙへ伝達されることとなり、暖房運転時における成績係数（ＣＯＰ）の低下を防止することができる。なお、温熱熱交換器５における２次冷媒ｙとの熱交換により冷却された中間濃溶液ｂは、分岐回路３９を介して高温再生器１へ還流される。
【００４８】
その他の構成および作用効果は第１の実施の形態におけると同様なので説明を省略する。
【００４９】
第２の参考例
図５には、第２の参考例にかかる空冷吸収式冷凍装置の全体的な冷凍システムの構成が示されている。
【００５０】
この場合、温熱熱交換器５と高温溶液熱交換器７とは一体化されて熱交換器ユニットＡとされている。該熱交換器ユニットＡは、図６に示すように、複数の伝熱プレート４１，４１・・を積層し、これらの伝熱プレート４１，４１・・間に通路４２Ａ，４２Ｂ・・を形成したプレート式熱交換器として構成されており、通路４２Ａ，４２Ｃに中間濃溶液ｂを流通させ、通路４２Ｂに吸収希溶液ｃを流通させ、通路４２Ｄに２次冷媒ｙを流通させるようにしている。このようにすれば、大幅なコストダウンを図ることができる。その他の構成および作用効果は第４の実施の形態におけると同様なので説明を省略する。
【００５１】
第３の参考例
図７には、第３の参考例にかかる空冷吸収式冷凍装置の全体的な冷凍システムの構成が示されている。
【００５２】
この場合、第２の参考例にかかる空冷吸収式冷凍装置における低温再生器６の吸収液通路６ａに第２の温熱熱交換器４３を配設している。また、冷暖切換弁２６，２７は、低温再生器６における吸収液通路６ａの上部から空冷凝縮器９へ至る配管４４および冷媒ポンプ１１から吸収液分配容器１６における散布装置１３へ至る配管４５から分岐して吸収液分配容器１６の底部に至る配管４６にそれぞれ介設されている。
【００５３】
上記のように構成したことにより、冷房運転時においては、冷暖切換弁２６を開弁し、冷暖切換弁２７を閉弁した状態で、高温再生器１を駆動させと、温熱熱交換器５には、気液分離器４により分離された中間濃溶液ｂが高温溶液熱交換器７を経て供給されることとなり、温熱熱交換器５の温度が１３０℃程度に抑えられることとなる。従って、温熱熱交換器５における２次冷媒ｙの異常過熱が防止されることとなり、２次冷媒ｙとして用いられているフロン系冷媒の分解が防止され、装置の信頼性を確保することができる。また、低温再生器６の吸収液通路６ａには、気液分離器４により分離された中間濃溶液ｂが高温溶液熱交換器７を経て供給されることとなり、吸収液通路６ａの温度は飽和蒸気（１００℃程度）と同等となる。従って、第２の温熱熱交換器４３の温度が１００℃程度に抑えられることとなり、第２の温熱熱交換器４３においても、２次冷媒ｙの異常過熱が防止される結果、２次冷媒ｙとして用いられているフロン系冷媒の分解が防止され、装置の信頼性を確保することができる。
【００５４】
一方、暖房運転時においては、冷暖切換弁２６を閉弁し、冷暖切換弁２７を開弁した状態で高温再生器１を駆動させと、温熱熱交換器５には、気液分離器４により分離された中間濃溶液ｂが高温溶液熱交換器７を経て供給され、温熱熱交換器５の温度は１３０℃程度となる。従って、暖房運転時において、温熱熱交換器５では気液分離器４から高温溶液熱交換器７を経て供給される吸収液（１３０℃程度）の保有する熱が暖房熱源として２次冷媒ｙへ伝達されるとともに、低温再生器６においては、気液分離器４から供給された水蒸気ａおよび温熱熱交換器５を経て供給された中間濃溶液ｂの保有する熱が暖房熱源として２次冷媒ｙに伝達される。従って、暖房運転時における成績係数（ＣＯＰ）の低下を防止することができる。なお、低温再生器６から出た凝縮水ｄは冷媒タンク１０、冷媒ポンプ１１を経て配管４６から吸収液分配容器１６の底部に送られる一方、中間濃溶液ｂは、そのまま冷媒分配容器１６の底部へ送られる。そして、冷媒分配容器１６において合流された凝縮水ｄと中間濃溶液ｂとは、空冷吸収器１５、溶液ポンプ１８、低温溶液熱交換器１４および高温溶液熱交換器７を経て気液分離器４へ還流される。
【００５５】
その他の構成および作用効果は第２の参考例におけると同様なので説明を省略する。
【００５６】
第４の実施の形態（請求項５、６に対応）
図８には、本願発明の第４の実施の形態にかかる空冷吸収式冷凍装置の全体的な冷凍システムの構成が示されている。
【００５７】
この場合、温熱熱交換器５と高温溶液熱交換器７とは一体化されて熱交換器ユニットＡとされている。該熱交換器ユニットＡは、図９に示すように、複数の伝熱プレート４１，４１・・を積層し、これらの伝熱プレート４１，４１・・間に通路４２Ａ，４２Ｂ・・を形成したプレート式熱交換器として構成されており、通路４２Ａ，４２Ｃに吸収吸収液ｃを流通させ、通路４２Ｂに中間濃溶液ｂを流通させ、通路４２Ｄに２次冷媒ｙを流通させるようにしている。また、高温溶液熱交換器７から低温再生器６に至る配管３８から分岐して低温溶液熱交換器１４と高温溶液熱交換器７との間の吸収希溶液配管４８に至る分岐回路４９が付設されており、該分岐回路４９には、冷房運転時に閉弁し、暖房運転時に開弁する開閉弁５０が介設されている。さらに、高温溶液熱交換器７から気液分離器４に至る吸収希溶液配管５１（換言すれば、温熱熱交換器５における１次冷媒通路）から分岐して高温再生器１に至る分岐回路５２が付設されており、該分岐回路５２には、前記温熱熱交換器５より高位であって前記気液分離器４と同一高さもしくはそれより低位に配置され且つ前記気液分離器４からの水蒸気ａが供給される暖房用吸収器５３が設けられている。符号５４は冷房運転時に開弁され、暖房運転時に閉弁する冷暖切換弁である。その他の構成は第２の参考例におけると同様なので説明を省略する。
【００５８】
上記のように構成したことにより、冷房運転時においては、冷暖切換弁２６，２７，５４を開弁し、開閉弁５０を閉弁した状態で高温再生器１を駆動させると、温熱熱交換器５には、気液分離器４により分離された中間濃溶液ｂが高温溶液熱交換器７を経て供給されることとなり、温熱熱交換器５の温度が１３０℃程度に抑えられることとなる。従って、温熱熱交換器５における２次冷媒ｙの異常過熱が防止されることとなり、２次冷媒ｙとして用いられているフロン系冷媒の分解が防止され、装置の信頼性を確保することができる。
【００５９】
一方、暖房運転時においては、冷暖切換弁２６，２７，５４を閉弁し、開閉弁５０を開弁した状態で高温再生器１を駆動させと、温熱熱交換器５には、気液分離器４により分離された中間濃溶液ｂが高温溶液熱交換器７を経て供給されるが、この時高温溶液熱交換器７には吸収希溶液ｃが供給されていないため、温熱熱交換器５の温度は１３０℃程度となる。従って、暖房運転時においては、気液分離器４から供給される吸収液（１３０℃程度）の保有する熱が暖房熱源として２次冷媒ｙへ伝達されることとなり、暖房運転時における成績係数（ＣＯＰ）の低下を防止することができる。なお、温熱熱交換器５における２次冷媒ｙとの熱交換により冷却された中間濃溶液ｂは、分岐回路４９、吸収希溶液配管４８、高温溶液熱交換器７、吸収希溶液配管５１および分岐回路５２を介して暖房吸収器５３に供給され、ここで、気液分離器４から供給された水蒸気ａを吸収して吸収希溶液ｃとなって高温再生器１へ還流される。このようにすると、暖房運転時における１次冷媒の搬送をスムーズに行うことができる。その他の作用効果は第２の参考例におけると同様なので説明を省略する。
【発明の効果】
【００６０】
本願発明の第１の基本構成によれば、冷房運転時において、暖房熱源を得るための温熱熱交換器５を低温再生器６の１次冷媒出口側と気液分離器４との間に接続するようにしているので、温熱熱交換器５の温度が飽和蒸気の温度（１００℃程度）に抑えられることとなり、温熱熱交換器５における２次冷媒ｙの異常過熱が防止され、２次冷媒ｙとして用いられているフロン系冷媒の分解が防止される結果、装置の信頼性を確保することができるという優れた効果がある。また、暖房運転時においては、気液分離器４から低温再生器６を経て温熱熱交換器５へ１次冷媒蒸気ａ（１３０℃程度）が供給されることとなっているので、該１次冷媒蒸気ａの保有する熱が暖房熱源として２次冷媒ｙへ伝達されることとなり、暖房運転時における成績係数（ＣＯＰ）の低下を防止することができるという効果もある。
【００６１】
本願発明の第１の基本構成において、前記凝縮液還流回路２１に、前記開閉弁２５に代えて液シール部３０を設けた場合、開閉弁２５を省略できることとなり、コストダウンに寄与する。
【００６２】
本願発明の第２の基本構成によれば、温熱熱交換器５の熱交換部を、低温再生器６における吸収液通路６ａに配設して、冷房運転時において、温熱熱交換器５の温度が１００℃程度に抑えられるようにしたので、温熱熱交換器５における２次冷媒ｙの異常過熱が防止され、２次冷媒ｙとして用いられているフロン系冷媒の分解が防止されることとなり、装置の信頼性を確保することができるという優れた効果がある。また、暖房運転時においては、気液分離器４から低温再生器６に供給される吸収液（１３０℃程度）の保有する熱が暖房熱源として２次冷媒ｙへ伝達されるようにしたので、暖房運転時における成績係数（ＣＯＰ）の低下を防止することができるという効果もある。
【００６３】
本願発明の第２の基本構成において、前記気液分離器４から前記低温再生器６へ供給される中間濃溶液ｂと前記空冷吸収器１５から前記気液分離器４へ還流される吸収希溶液ｃとを熱交換させる高温溶液熱交換器７と、前記中間濃溶液ｂが流通する配管３１に、前記高温溶液熱交換器７をバイパスし且つ暖房運転時にのみ開通するバイパス回路３２とを設けた場合、暖房運転時において低温再生器６へは高温溶液熱交換器７をバイパスした（即ち、高温溶液熱交換器７において吸収希溶液ｃに熱回収されない）中間濃溶液ｂが供給されることとなり、冷房運転時における高温再生器１へ還流される吸収希溶液ｃへの熱回収を有効に行いつつ、暖房運転時における成績係数（ＣＯＰ）の低下を防止することができる。
【００６４】
本願発明の第３の基本構成によれば、気液分離器４から低温再生器６へ供給される中間濃溶液ｂと空冷吸収器１５から前記気液分離器４へ還流される吸収希溶液ｃとを熱交換させる高温溶液熱交換器７の下流側に温熱熱交換器５を配設して、冷房運転時において、温熱熱交換器５の温度が高温溶液熱交換器７の下流側の吸収液温度１３０℃程度と同等に抑えられるようにしたので、温熱熱交換器５における２次冷媒ｙの異常過熱が防止され、２次冷媒ｙとして用いられているフロン系冷媒の分解が防止されることとなり、装置の信頼性を確保することができるという優れた効果がある。また、暖房運転時においては、気液分離器４から高温溶液熱交換器７を通過した中間濃溶液ｂ（１３０℃程度）の保有する熱が暖房熱源として２次冷媒ｙへ伝達されるようにしたので、暖房運転時における成績係数（ＣＯＰ）の低下を防止することができるという効果もある。しかも、暖房運転時において温熱熱交換器５の１次冷媒通路に供給された吸収濃溶液ｂが暖房吸収器５３に入り、そこで１次冷媒蒸気ａを吸収して吸収希溶液ｃとなって高温再生器１へ還流されるようにしているので、暖房運転時における１次冷媒の搬送をスムーズに行うことができるという効果もある。
【００６５】
本願発明の第３の基本構成において、前記温熱熱交換器５と前記高温溶液熱交換器７とを一体化した場合、コストダウンを図ることができる。
【図面の簡単な説明】
【図１】本願発明の第１の実施の形態にかかる空冷吸収式冷凍装置の冷凍サイクルを示す回路図である。
【図２】本願発明の第２の実施の形態にかかる空冷吸収式冷凍装置の冷凍サイクルを示す回路図である。
【図３】本願発明の第３の実施の形態にかかる空冷吸収式冷凍装置の冷凍サイクルを示す回路図である。
【図４】本願発明の第１の参考例にかかる空冷吸収式冷凍装置の冷凍サイクルを示す回路図である。
【図５】本願発明の第２の参考例にかかる空冷吸収式冷凍装置の冷凍サイクルを示す回路図である。
【図６】本願発明の第２の参考例にかかる空冷吸収式冷凍装置における熱交換器ユニットの内部を透視した斜視図である。
【図７】本願発明の第３の参考例にかかる空冷吸収式冷凍装置の冷凍サイクルを示す回路図である。
【図８】本願発明の第４の実施の形態にかかる空冷吸収式冷凍装置の冷凍サイクルを示す回路図である。
【図９】本願発明の第４の実施の形態にかかる空冷吸収式冷凍装置における熱交換器ユニットの内部を透視した斜視図である。
【符号の説明】
１は高温再生器、４は気液分離器、５は温熱熱交換器、６は低温再生器、６ａは吸収液通路、９は空冷凝縮器、１１は冷媒ポンプ、１２は蒸発器、１５は空冷吸収器、１７は利用側熱交換器、１８は溶液ポンプ、２１は凝縮液還流回路、２５は開閉弁、３０は液シール部、３２はバイパス回路、３３は開閉弁、４３は第２の温熱熱交換器、５３は暖房用吸収器、ａは１次冷媒蒸気（水蒸気）、ｂは吸収濃溶液（臭化リチウム濃溶液）、ｃは吸収希溶液（臭化リチウム希溶液）、ｄは１次冷媒凝縮液（凝縮水）、Ｘは１次冷媒回路、Ｙは２次冷媒回路、ｙは２次冷媒。[0001]
BACKGROUND OF THE INVENTION
[0002]
  The present invention relates to an air-cooled absorption refrigeration apparatus, and more particularly to a mechanism for preventing overheating of a secondary refrigerant in the air-cooled absorption refrigeration apparatus.
[Prior art]
[0003]
  In general, in an air-cooled absorption refrigeration apparatus, a primary refrigerant circulates, a regenerator, a gas-liquid separator, a thermal heat exchanger that obtains a heating heat source from a primary refrigerant (for example, primary refrigerant vapor), an air-cooled condenser, A primary refrigerant circuit formed by connecting an evaporator that obtains a cooling heat source from a secondary refrigerant (for example, a condensed primary refrigerant liquid) and an air-cooled absorber, and a secondary refrigerant circulate, and the thermal heat exchanger and the use side heat exchange. And a secondary refrigerant circuit formed by connecting the evaporator and the evaporator.
[Problems to be solved by the invention]
[0004]
  In the case of the air-cooled absorption refrigeration apparatus configured as described above, the heat held by the high-temperature primary refrigerant vapor supplied from the gas-liquid separator as a heating heat source during heating operation is transmitted to the secondary refrigerant by the thermal heat exchanger. Thus, even during the cooling operation, the secondary refrigerant flowing through the thermal heat exchanger is exposed to the high-temperature primary refrigerant vapor. In this case, in the air-cooled absorption refrigeration apparatus using water as the secondary refrigerant, there is not much problem except that the water circulating in the secondary refrigerant circuit may become high pressure. In addition, in order to prevent high pressure of circulating water, there exists what connected the evaporator from which cold water is obtained, and a thermal heat exchanger in series.
[0005]
  However, in the case where a chlorofluorocarbon refrigerant (for example, a mixed refrigerant such as R407c) is used as the secondary refrigerant, if the air-cooled absorption refrigeration apparatus is kept as described above, a high-temperature primary refrigerant is added to the thermal heat exchanger during the cooling operation. Since steam (150 ° C. or higher) is supplied, the chlorofluorocarbon refrigerant as the secondary refrigerant is exposed to a high temperature. Then, the malfunction that a fluorocarbon refrigerant will decompose | disassemble will arise.
[0006]
  The present invention has been made in view of the above points, and by preventing abnormal overheating of the secondary refrigerant during cooling operation, even if a chlorofluorocarbon refrigerant is used as the secondary refrigerant, refrigerant decomposition does not occur. It is intended to do.
[Means for Solving the Problems]
[0007]
  In the first basic configuration of the present invention, as means for solving the above-described problem, the primary refrigerant circulates, the high-temperature regenerator 1, the gas-liquid separator 4, and the thermal heat exchanger 5 for obtaining a heating heat source, A primary refrigerant circuit X in which a low-temperature regenerator 6, an air-cooled condenser 9, an evaporator 12 for obtaining a cooling heat source, and an air-cooled absorber 15 are sequentially connected, and a secondary refrigerant y circulates, and the thermal heat exchanger. 5. In an air-cooled absorption refrigeration apparatus comprising a secondary refrigerant circuit Y formed by sequentially connecting the use side heat exchanger 17 and the evaporator 12, a fluorocarbon refrigerant is used as the secondary refrigerant y, andThe thermal heat exchanger 5 is interposed between the primary refrigerant outlet in the low temperature regenerator 6 and the gas-liquid separator 4, and the thermal heat exchanger 5The condensate reflux circuit 21 that is in communication is provided with an open / close valve 25 that closes during cooling operation and opens during heating operation.
[0008]
  By configuring as described above, during the cooling operation, steam (about 100 ° C.) that has passed through the low temperature regenerator 6 and saturated flows into the heat heat exchanger 5, so that the temperature of the heat heat exchanger 5 is It will be suppressed to about 100 ° C. Accordingly, abnormal overheating of the secondary refrigerant y in the thermal heat exchanger 5 is prevented, and decomposition of the chlorofluorocarbon refrigerant used as the secondary refrigerant y is prevented, thereby ensuring the reliability of the apparatus. . Further, during the heating operation, the primary refrigerant vapor a (about 130 ° C.) is supplied from the gas-liquid separator 4 through the low-temperature regenerator 6 to the thermal heat exchanger 5, and the primary refrigerant vapor a The retained heat is transmitted to the secondary refrigerant y as a heating heat source. Accordingly, it is possible to prevent a decrease in the coefficient of performance (COP) during the heating operation.
[0009]
  In the first basic configuration of the present invention, the condensaterefluxWhen the circuit 21 is provided with the liquid seal portion 30 instead of the on-off valve 25, the on-off valve 25 can be omitted, which contributes to cost reduction.
[0010]
  In the second basic configuration of the present invention, as means for solving the above problems, the primary refrigerant circulates, the high-temperature regenerator 1, the gas-liquid separator 4, and the thermal heat exchanger 5 for obtaining a heating heat source, A primary refrigerant circuit X in which a low-temperature regenerator 6, an air-cooled condenser 9, an evaporator 12 for obtaining a cooling heat source, and an air-cooled absorber 15 are sequentially connected, and a secondary refrigerant y circulates, and the thermal heat exchanger. 5. In an air-cooled absorption refrigeration apparatus comprising a secondary refrigerant circuit Y formed by sequentially connecting the use side heat exchanger 17 and the evaporator 12, a fluorocarbon refrigerant is used as the secondary refrigerant y, andThe heat exchange part of the thermal heat exchanger 5 in which the secondary refrigerant y is supplied to the absorbing liquid passage 6a in the low temperature regenerator 6 is provided.It is arranged.
[0011]
  By configuring as described above, the temperature of the heat exchanger 5 is about 100 ° C. during the cooling operation because the absorption liquid temperature in the low-temperature regenerator 6 is equivalent to saturated steam (about 100 ° C.). Will be suppressed. Accordingly, abnormal overheating of the secondary refrigerant y in the thermal heat exchanger 5 is prevented, and decomposition of the chlorofluorocarbon refrigerant used as the secondary refrigerant y is prevented, thereby ensuring the reliability of the apparatus. . Further, during the heating operation, the heat held by the absorbing liquid (about 130 ° C.) supplied from the gas-liquid separator 4 to the low-temperature regenerator 6 is transmitted to the secondary refrigerant y as a heating heat source. Accordingly, it is possible to prevent a decrease in the coefficient of performance (COP) during the heating operation.
[0012]
  In the second basic configuration of the present invention, an intermediate concentrated solution supplied from the gas-liquid separator 4 to the low-temperature regenerator 6 and an absorbing dilute solution refluxed from the air-cooled absorber 15 to the gas-liquid separator 4 When the high-temperature solution heat exchanger 7 that exchanges heat is provided and the bypass circuit 32 that bypasses the high-temperature solution heat exchanger 7 and is opened only during the heating operation is provided in the pipe through which the intermediate concentrated solution flows. At that time, the high temperature solution heat exchanger 7 is bypassed to the low temperature regenerator 6 (that is, the intermediate concentrated solution b is not recovered by the high temperature solution heat exchanger 7 in the absorbed dilute solution c). In this case, it is possible to prevent a decrease in the coefficient of performance (COP) during the heating operation while effectively recovering the heat to the absorbing dilute solution c refluxed to the high temperature regenerator 1.
[0013]
  In the third basic configuration of the present invention, as means for solving the above problems, the primary refrigerant circulates, the high-temperature regenerator 1, the gas-liquid separator 4, and the thermal heat exchanger 5 for obtaining a heating heat source, A primary refrigerant circuit X in which a low-temperature regenerator 6, an air-cooled condenser 9, an evaporator 12 for obtaining a cooling heat source, and an air-cooled absorber 15 are sequentially connected, and a secondary refrigerant y circulates, and the thermal heat exchanger. 5. In an air-cooled absorption refrigeration apparatus comprising a secondary refrigerant circuit Y formed by sequentially connecting the use side heat exchanger 17 and the evaporator 12, a fluorocarbon refrigerant is used as the secondary refrigerant y, and A high-temperature solution heat exchanger for exchanging heat between the intermediate concentrated solution b supplied from the gas-liquid separator 4 to the low-temperature regenerator 6 and the absorption diluted solution c refluxed from the air-cooled absorber 15 to the gas-liquid separator 4 7 and the downstream side of the high-temperature solution heat exchanger 7 Provided the heat exchanger 5On the other hand, the outlet of the primary refrigerant passage in the thermal heat exchanger 5 is supplied with the primary refrigerant vapor a from the gas-liquid separator 4 and is higher than the thermal heat exchanger 5 so that the gas-liquid Connected to the high-temperature regenerator 1 through a heating absorber 53 arranged at the same height as the separator 4 or lower than the separator 4is doing.
[0014]
  With the above configuration, during cooling operation, the absorption liquid temperature downstream of the high temperature solution heat exchanger 7 is about 130 ° C. due to heat recovery in the high temperature solution heat exchanger 7, The temperature of the exchanger 5 is suppressed to about 130 ° C. Accordingly, abnormal overheating of the secondary refrigerant y in the thermal heat exchanger 5 is prevented, and decomposition of the chlorofluorocarbon refrigerant used as the secondary refrigerant y is prevented, thereby ensuring the reliability of the apparatus. . Further, during heating operation, heat held by the intermediate concentrated solution b (about 130 ° C.) that has passed through the high-temperature solution heat exchanger 7 from the gas-liquid separator 4 is transmitted to the secondary refrigerant y as a heating heat source. Become. Accordingly, it is possible to prevent a decrease in the coefficient of performance (COP) during the heating operation.In addition, the absorption concentrated solution b supplied to the primary refrigerant passage of the thermal heat exchanger 5 during the heating operation enters the heating absorber 53, where it absorbs the primary refrigerant vapor a to become an absorption diluted solution c and has a high temperature. Since it is made to recirculate | reflux to the regenerator 1, the conveyance of the primary refrigerant | coolant at the time of heating operation can be performed smoothly.
[0015]
  In the third basic configuration of the present invention, when the thermal heat exchanger 5 and the high-temperature solution heat exchanger 7 are integrated, the cost can be reduced.
DETAILED DESCRIPTION OF THE INVENTION
[0016]
  Hereinafter, some preferred embodiments of the present invention will be described with reference to the accompanying drawings.And reference examplesWill be described in detail.
[0017]
  The following embodimentsAnd reference examples, A lithium bromide aqueous solution (LiBr aqueous solution) is used as the absorbing liquid, water and water vapor are used as the primary refrigerant circulating in the primary refrigerant circuit X, and the secondary refrigerant y circulating in the secondary refrigerant circuit Y is used. CFC-based refrigerant (for example, mixed refrigerant such as R407c) is employed.
[0018]
  First embodiment (corresponding to claim 1)
  FIG. 1 shows an overall refrigeration system configuration of an air-cooled absorption refrigeration apparatus according to a first embodiment of the present invention.
[0019]
  In FIG. 1, reference numeral 1 denotes a high-temperature regenerator, which includes a heating source 2 such as a gas burner. Above the high-temperature regenerator 1, a gas-liquid separator 4 communicated via a boiling gas-liquid passage 3 is provided. In the high-temperature regenerator 1, the absorption dilute solution c (that is, lithium bromide dilute solution) is heated and boiled and supplied to the gas-liquid separator 4 positioned above through the boiling gas-liquid passage 3. It is separated and regenerated into water vapor a which is the primary refrigerant vapor and absorption concentrated solution b (that is, lithium bromide concentrated solution).
[0020]
  The lithium bromide dilute solution c is obtained by absorbing water d, which is the primary refrigerant condensate, into the lithium bromide concentrated solution b, which is an absorption concentrated solution, in an air-cooled absorber 15 which will be described in detail later. It is preheated via the condenser 14 and the high-temperature solution heat exchanger 7 and supplied to the gas-liquid separator 4, and then refluxed to the high-temperature regenerator 1.
[0021]
  The water vapor a separated in the gas-liquid separator 4 is sent to the low temperature regenerator 6. On the other hand, the intermediate concentrated solution b of lithium bromide separated in the gas-liquid separator 4 is heat-exchanged with the dilute lithium bromide c in the high-temperature solution heat exchanger 7 and then absorbed by the low-temperature regenerator 6. It is supplied to the liquid passage 6a. The temperature of the intermediate concentrated solution b supplied to the low-temperature regenerator 6 is about 130 ° C. Reference numeral 8 denotes an exhaust gas passage for discharging exhaust gas.
[0022]
  In the low-temperature regenerator 6, the water vapor a supplied from the gas-liquid separator 4 and the intermediate concentrated solution b are subjected to heat exchange, thereby condensing the water vapor a and evaporating residual water contained in the intermediate concentrated solution b. Then, a higher concentration lithium bromide solution is taken out.
[0023]
  The water vapor a evaporated from the intermediate concentrated solution b in the low-temperature regenerator 6 is sent to the air-cooled condenser 9 where it is condensed and liquefied to become a primary refrigerant condensate (ie, condensed water d) and stored in the refrigerant tank 10. Further, the condensed water d condensed and liquefied in the low-temperature regenerator 6 joins at the lower end of the air-cooled condenser 9 and is then stored in the refrigerant tank 10. Note that the steam a exiting the low temperature regenerator 6 is saturated steam (about 100 ° C.).
[0024]
  The condensed water d stored in the refrigerant tank 10 is supplied to the spraying device 13 of the evaporator 12 by the refrigerant pump 11. Further, the concentrated lithium bromide solution b taken out from the low-temperature regenerator 6 is heat-exchanged with the above-described diluted lithium bromide solution c in the low-temperature solution heat exchanger 14, and then stored in the absorbent distribution container 16 of the air-cooled absorber 15. Supplied.
[0025]
  The evaporator 12 exchanges heat between the secondary refrigerant y (for example, R407C) circulating in the secondary refrigerant circuit Y including the use side heat exchanger 17 and the condensed water d sent from the refrigerant tank 10. It acts to obtain a cold source during cooling operation. The condensed water d that has not been evaporated in the evaporator 12 is returned to the upstream side of the refrigerant pump 11 via the condensed water recirculation circuit 29.
[0026]
  Then, the lithium bromide dilute solution c taken out from the air-cooled absorber 15 is returned to the gas-liquid separator 4 by the solution pump 18 through the low-temperature solution heat exchanger 14 and the high-temperature solution heat exchanger 7 as described above. .
[0027]
  Therefore, in the present embodiment, thermal heat exchange for obtaining a heating heat source between the primary refrigerant outlet (in other words, the steam outlet 6b) in the low-temperature regenerator 6 and the gas-liquid separator 4 is performed. A heat exchanger 5 is interposed between the thermal heat exchanger 5 and the gas-liquid separator 4.TheAn open / close valve 25 that closes during cooling operation and opens during heating operation is interposed in the condensate reflux circuit 21 that communicates. The thermal heat exchanger 5 includes a secondary refrigerant y (for example, R407c) that circulates in a secondary refrigerant circuit Y including a use-side heat exchanger 17 that will be described in detail later, and saturated steam (100 ° C.) that has passed through the low-temperature regenerator 6. Exchanges heat and obtains a heat source during heating operation. Then, the primary refrigerant condensate d (that is, condensed water) condensed in the thermal heat exchanger 5 is refluxed to the gas-liquid separator 4 via the condensate reflux circuit 21. It should be noted that an opening / closing valve that is closed during the cooling operation and opened during the heating operation may be provided in the pipe extending from the steam outlet 6b of the low-temperature regenerator 6 to the thermal heat exchanger 5. As the thermal heat exchanger 5, a shell and coil heat exchanger, a shell and tube heat exchanger, a double tube heat exchanger, a plate heat exchanger, or the like is employed.
[0028]
  In the drawings, reference numerals 26 and 27 denote cooling / heating switching valves, which are opened during cooling operation and closed during heating operation.
[0029]
  The air-cooled absorption refrigeration apparatus configured as described above operates as follows.
(I) During cooling operation
  When the on-off valve 25 is closed and the cooling / heating switching valves 26 and 27 are opened, when the high-temperature regenerator 1 is operated by igniting the gas burner 2 as a heating source, the boiling gas / liquid is supplied to the gas / liquid separator 4. Where the water vapor a is separated into the intermediate concentrated solution b of lithium bromide, the water vapor a is heated to the low temperature regenerator 6, and the intermediate concentrated solution b is heated to the lithium bromide diluted solution c in the high temperature solution heat exchanger 7. After that, it is supplied to the low temperature regenerator 6.
[0030]
  In the low temperature regenerator 6, the intermediate concentrated solution b is heated by heat exchange with the water vapor a to evaporate the water vapor a and further concentrate itself. Here, the condensed water d condensed by heat exchange with the intermediate concentrated solution b is stored in the refrigerant tank 10 through the lower part of the air-cooled condenser 9. On the other hand, the water vapor a evaporated from the intermediate concentrated solution b in the low-temperature regenerator 6 is condensed in the air-cooled condenser 9 to become condensed water d and stored in the refrigerant tank 10.
[0031]
  Condensed water d stored in the refrigerant tank 10 is supplied to the spraying device 13 by the refrigerant pump 11 and then sprayed to the evaporator 12, where it evaporates itself by exchanging heat with the secondary refrigerant y. The secondary refrigerant y is cooled. The secondary refrigerant y thus cooled is used as a cooling heat source for cooling in the use-side heat exchanger 17.
[0032]
  On the other hand, the concentrated lithium bromide solution b taken out from the low-temperature regenerator 6 is heat-exchanged with the above-described diluted lithium bromide solution c in the low-temperature solution heat exchanger 14, and then passes through the absorption liquid distribution container 16 and the air-cooled absorber 15. The water vapor a obtained by the evaporator 12 is absorbed and becomes a lithium bromide dilute solution c.
[0033]
  The lithium bromide dilute solution c taken out from the air-cooled absorber 15 is preheated by the solution pump 18 in the process of passing through the low-temperature solution heat exchanger 14 and the high-temperature solution heat exchanger 7 as described above, and gas-liquid separation is performed. Returned to vessel 4.
[0034]
  As described above, during cooling operation, the saturated water vapor a (about 100 ° C.) that has passed through the low-temperature regenerator 6 flows into the thermal heat exchanger 5, so the temperature of the thermal heat exchanger 5 is about 100 ° C. Will be suppressed. Accordingly, abnormal overheating of the secondary refrigerant y in the thermal heat exchanger 5 is prevented, and decomposition of the chlorofluorocarbon refrigerant used as the secondary refrigerant y is prevented, thereby ensuring the reliability of the apparatus. .
(II) During heating operation
  When the gas burner 2 as a heating source is ignited and the high temperature regenerator 1 is operated in a state where the on-off valve 25 is opened and the cooling / heating switching valves 26 and 27 are closed, the boiling gas / liquid is transferred to the gas / liquid separator 4. The water vapor a and the intermediate concentrated solution b of lithium bromide are separated, and the water vapor a is supplied to the thermal heat exchanger 5 through the low-temperature regenerator 6.
[0035]
  In the thermal heat exchanger 5, the saturated water vapor a is condensed by heat exchange with the secondary refrigerant y, and the obtained condensed water is refluxed to the gas-liquid separator 4 through the condensate circulation circuit 21. Returned to the high temperature regenerator 1. That is, the heat possessed by the saturated water vapor a is given to the secondary refrigerant y as a heating heat source.
[0036]
  As described above, during the heating operation, the saturated water vapor a output from the low temperature regenerator 6 is supplied to the thermal heat exchanger 5, and the heat held by the saturated water vapor a is transmitted to the secondary refrigerant y as a heating heat source. The Rukoto. Accordingly, it is possible to prevent a decrease in the coefficient of performance (COP) during the heating operation.
[0037]
  Second Embodiment (BillingItem 2Corresponding to)
  FIG. 2 shows an overall refrigeration system configuration of an air-cooled absorption refrigeration apparatus according to a second embodiment of the present invention.
[0038]
  In this case, the condensate reflux circuit 21 that connects the thermal heat exchanger 5 and the gas-liquid separator 4 is provided with a liquid seal portion 30 formed of a U-shaped tube instead of the on-off valve 25. The liquid seal part 30 encloses the condensed water condensed in the thermal heat exchanger 5 during the cooling operation, and saturated steam is short-circuited from the low-temperature regenerator 6 to the gas-liquid separator 4 via the thermal heat exchanger 5. This is equivalent to an on-off valve. This eliminates the need for an on-off valve and contributes to cost reduction. Since other configurations and operational effects are the same as those in the first embodiment, description thereof will be omitted.
[0039]
  Third embodiment (corresponding to claims 3 and 4)
  FIG. 3 shows an overall refrigeration system configuration of an air-cooled absorption refrigeration apparatus according to a third embodiment of the present invention.
[0040]
  In this case, the thermal heat exchanger 5Heat exchangerIs disposed in the absorbent passage 6 a in the low-temperature regenerator 6. Further, the cooling / heating switching valve 26 is omitted, and a bypass circuit 32 that bypasses the high-temperature solution heat exchanger 7 and opens only during the heating operation is provided in the pipe 31 through which the intermediate concentrated solution b flows. The bypass circuit 32 is provided with an open / close valve 33 that closes during cooling operation and opens during heating operation. Further, a branch circuit 35 branched from the pipe 34 extending from the low temperature regenerator 6 to the low temperature solution heat exchanger 14 and leading to the high temperature regenerator 1 is attached. The branch circuit 35 is closed during cooling operation, An on-off valve 36 that opens during heating operation is interposed. Reference numeral 37 denotes an on-off valve for switching between cooling and heating, which is provided in a pipe extending from the low-temperature solution heat exchanger 14 to the absorbing liquid distribution container 16.
[0041]
  With the above configuration, during the cooling operation, the on-off valves 33 and 36 are closed, and the high temperature regenerator 1 is driven with the cooling / heating switching valve 27 and the on-off valve 37 opened. Then, the intermediate concentrated solution b separated by the gas-liquid separator 4 is supplied to the absorption liquid passage 6a of the low temperature regenerator 6 via the high temperature solution heat exchanger 7, and the temperature of the absorption liquid passage 6a is saturated. Equivalent to steam (about 100 ° C). Therefore, the temperature of the thermal heat exchanger 5 is suppressed to about 100 ° C., and the abnormal overheating of the secondary refrigerant y in the thermal heat exchanger 5 is prevented. As a result, the chlorofluorocarbon refrigerant used as the secondary refrigerant y. Can be prevented, and the reliability of the apparatus can be ensured.
[0042]
  On the other hand, during the heating operation, the cooling / heating switching valve 27 and the on-off valve 37 are closed, and the high-temperature regenerator 1 is driven with the on-off valves 33 and 36 opened. Then, the intermediate concentrated solution b separated by the gas-liquid separator 4 is directly supplied to the absorption liquid passage 6a of the low temperature regenerator 6, and the temperature of the absorption liquid passage 6a becomes about 130 ° C. Accordingly, during the heating operation, the heat held in the absorbing liquid (about 130 ° C.) supplied from the gas-liquid separator 4 to the low-temperature regenerator 6 is transmitted to the secondary refrigerant y as a heating heat source, and the heating operation is performed. Decrease in coefficient of performance (COP) at the time can be prevented. The intermediate concentrated solution b cooled by heat exchange with the secondary refrigerant y in the low temperature regenerator 6 is returned to the high temperature regenerator 1 through the pipe 34 and the branch circuit 35.
[0043]
  Since other configurations and operational effects are the same as those in the first embodiment, description thereof will be omitted.
[0044]
  First reference example
  In FIG.First reference exampleThe structure of the whole refrigeration system of the air-cooled absorption refrigeration apparatus concerning this is shown.
[0045]
  In this case, the thermal heat exchanger 5 is disposed on the downstream side of the high-temperature solution heat exchanger 7. Further, a branch circuit 39 that branches from the upstream side of the cooling / heating switching valve 26 in the pipe 38 extending from the thermal heat exchanger 5 to the low temperature regenerator 6 and reaches the high temperature regenerator 1 is attached. Further, an on-off valve 40 that is closed during the cooling operation and opened during the heating operation is interposed.
[0046]
  By configuring as described above, during the cooling operation, the on-off valve 40 is closed, and the high temperature regenerator 1 is driven with the cooling / heating switching valves 26 and 27 opened. Then, the intermediate concentrated solution b separated by the gas-liquid separator 4 is supplied to the thermal heat exchanger 5 via the high temperature solution heat exchanger 7, and the temperature of the thermal heat exchanger 5 is changed to the high temperature solution heat exchange. It will be suppressed to about 130 ° C. by heat recovery in the vessel 7. Accordingly, abnormal overheating of the secondary refrigerant y in the thermal heat exchanger 5 is prevented, and decomposition of the chlorofluorocarbon refrigerant used as the secondary refrigerant y is prevented, and the reliability of the apparatus can be ensured. .
[0047]
  On the other hand, during the heating operation, the high-temperature regenerator 1 is driven with the cooling / heating switching valves 26 and 27 closed and the on-off valve 40 opened. Then, the hot concentrated heat exchanger 5 is supplied with the intermediate concentrated solution b separated by the gas-liquid separator 4 via the high temperature solution heat exchanger 7. At this time, the hot diluted solution is supplied to the high temperature solution heat exchanger 7. Since c is not supplied, the temperature of the thermal heat exchanger 5 is about 130 ° C. Therefore, during the heating operation, the heat held by the absorbing liquid (about 130 ° C.) supplied from the gas-liquid separator 4 is transmitted to the secondary refrigerant y as a heating heat source, and the coefficient of performance ( COP) can be prevented from decreasing. The intermediate concentrated solution b cooled by heat exchange with the secondary refrigerant y in the thermal heat exchanger 5 is returned to the high temperature regenerator 1 via the branch circuit 39.
[0048]
  Since other configurations and operational effects are the same as those in the first embodiment, description thereof will be omitted.
[0049]
  Second reference example
  In FIG.Second reference exampleThe structure of the whole refrigeration system of the air-cooled absorption refrigeration apparatus concerning this is shown.
[0050]
  In this case, the thermal heat exchanger 5 and the high temperature solution heat exchanger 7 are integrated into a heat exchanger unit A. As shown in FIG. 6, the heat exchanger unit A is formed by stacking a plurality of heat transfer plates 41, 41,... And forming passages 42A, 42B,. The plate-type heat exchanger is configured such that the intermediate concentrated solution b is circulated through the passages 42A and 42C, the absorption diluted solution c is circulated through the passage 42B, and the secondary refrigerant y is circulated through the passage 42D. In this way, significant cost reduction can be achieved. Since other configurations and operational effects are the same as those in the fourth embodiment, the description thereof is omitted.
[0051]
  Third reference example
  In FIG.Third reference exampleThe structure of the whole refrigeration system of the air-cooled absorption refrigeration apparatus concerning this is shown.
[0052]
  in this case,Second reference exampleIn the air-cooled absorption refrigeration apparatus, a second thermal heat exchanger 43 is disposed in the absorbing liquid passage 6a of the low-temperature regenerator 6. The cooling / heating switching valves 26 and 27 are branched from a pipe 44 extending from the upper part of the absorbing liquid passage 6a in the low temperature regenerator 6 to the air cooling condenser 9 and a pipe 45 extending from the refrigerant pump 11 to the spraying device 13 in the absorbing liquid distribution container 16. Thus, the pipes 46 are respectively provided to the bottom of the absorbent liquid distribution container 16.
[0053]
  With the above configuration, during the cooling operation, when the high temperature regenerator 1 is driven with the cooling / heating switching valve 26 opened and the cooling / heating switching valve 27 closed, the thermal heat exchanger 5 is turned on. The intermediate concentrated solution b separated by the gas-liquid separator 4 is supplied via the high-temperature solution heat exchanger 7, and the temperature of the thermal heat exchanger 5 is suppressed to about 130 ° C. Accordingly, abnormal overheating of the secondary refrigerant y in the thermal heat exchanger 5 is prevented, and decomposition of the chlorofluorocarbon refrigerant used as the secondary refrigerant y is prevented, and the reliability of the apparatus can be ensured. . Further, the intermediate concentrated solution b separated by the gas-liquid separator 4 is supplied to the absorption liquid passage 6a of the low temperature regenerator 6 via the high temperature solution heat exchanger 7, and the temperature of the absorption liquid passage 6a is saturated. Equivalent to steam (about 100 ° C). Therefore, the temperature of the second thermal heat exchanger 43 is suppressed to about 100 ° C., and in the second thermal heat exchanger 43, the secondary refrigerant y is prevented from being overheated abnormally. As a result, it is possible to prevent decomposition of the chlorofluorocarbon-based refrigerant used in the above, and to ensure the reliability of the apparatus.
[0054]
  On the other hand, during the heating operation, when the high temperature regenerator 1 is driven with the cooling / heating switching valve 26 closed and the cooling / heating switching valve 27 opened, the thermal heat exchanger 5 is connected to the gas / liquid separator 4. The separated intermediate concentrated solution b is supplied through the high temperature solution heat exchanger 7, and the temperature of the heat heat exchanger 5 becomes about 130 ° C. Therefore, during the heating operation, in the thermal heat exchanger 5, the heat held in the absorbing liquid (about 130 ° C.) supplied from the gas-liquid separator 4 via the high-temperature solution heat exchanger 7 is used as the heating heat source to the secondary refrigerant y. In the low-temperature regenerator 6, the steam a supplied from the gas-liquid separator 4 and the heat stored in the intermediate concentrated solution b supplied via the thermal heat exchanger 5 are used as a heating heat source for the secondary refrigerant y. Is transmitted to. Accordingly, it is possible to prevent a decrease in the coefficient of performance (COP) during the heating operation. Condensed water d discharged from the low-temperature regenerator 6 passes through the refrigerant tank 10 and the refrigerant pump 11 and is sent from the pipe 46 to the bottom of the absorbent distribution container 16, while the intermediate concentrated solution b remains as it is at the bottom of the refrigerant distribution container 16. Sent to. The condensed water d and the intermediate concentrated solution b merged in the refrigerant distribution container 16 pass through the air-cooled absorber 15, the solution pump 18, the low-temperature solution heat exchanger 14, and the high-temperature solution heat exchanger 7, and the gas-liquid separator 4. To reflux.
[0055]
  Other configurations and effects areSecond reference exampleSince it is the same as in FIG.
[0056]
  First4Embodiment (Claim 5), 6Corresponding to)
  FIG. 8 shows the first aspect of the present invention.4The structure of the whole refrigeration system of the air cooling absorption refrigeration apparatus concerning this embodiment is shown.
[0057]
  In this case, the thermal heat exchanger 5 and the high temperature solution heat exchanger 7 are integrated into a heat exchanger unit A. As shown in FIG. 9, the heat exchanger unit A is formed by laminating a plurality of heat transfer plates 41, 41,... And forming passages 42A, 42B,. The plate-type heat exchanger is configured such that the absorption / absorption liquid c flows through the passages 42A and 42C, the intermediate concentrated solution b flows through the passage 42B, and the secondary refrigerant y flows through the passage 42D. Further, a branch circuit 49 branching from a pipe 38 extending from the high temperature solution heat exchanger 7 to the low temperature regenerator 6 and leading to an absorption dilute solution pipe 48 between the low temperature solution heat exchanger 14 and the high temperature solution heat exchanger 7 is attached. The branch circuit 49 is provided with an on-off valve 50 that closes during cooling operation and opens during heating operation. Further, a branch circuit 52 that branches from the high-temperature solution heat exchanger 7 to the gas-liquid separator 4 (in other words, the primary refrigerant passage in the heat-heat exchanger 5) branches to the high-temperature regenerator 1. The branch circuit 52 is disposed at a level higher than the thermal heat exchanger 5 and at the same height as or lower than the gas-liquid separator 4 and from the gas-liquid separator 4. A heating absorber 53 to which water vapor a is supplied is provided. Reference numeral 54 is a cooling / heating switching valve that is opened during the cooling operation and closed during the heating operation. Other configurations areSecond reference exampleSince it is the same as in FIG.
[0058]
  With the above configuration, during the cooling operation, when the high-temperature regenerator 1 is driven with the cooling / heating switching valves 26, 27, 54 opened and the on-off valve 50 closed, the thermal heat exchanger 5, the intermediate concentrated solution b separated by the gas-liquid separator 4 is supplied via the high-temperature solution heat exchanger 7, and the temperature of the thermal heat exchanger 5 is suppressed to about 130 ° C. Accordingly, abnormal overheating of the secondary refrigerant y in the thermal heat exchanger 5 is prevented, and decomposition of the chlorofluorocarbon refrigerant used as the secondary refrigerant y is prevented, and the reliability of the apparatus can be ensured. .
[0059]
  On the other hand, during the heating operation, when the high-temperature regenerator 1 is driven with the cooling / heating switching valves 26, 27, 54 closed and the on-off valve 50 opened, the thermal heat exchanger 5 has a gas-liquid separation. The intermediate concentrated solution b separated by the vessel 4 is supplied through the high-temperature solution heat exchanger 7, but at this time, the absorption-dilute solution c is not supplied to the high-temperature solution heat exchanger 7. The temperature is about 130 ° C. Therefore, during the heating operation, the heat held by the absorbing liquid (about 130 ° C.) supplied from the gas-liquid separator 4 is transmitted to the secondary refrigerant y as a heating heat source, and the coefficient of performance ( COP) can be prevented from decreasing. The intermediate concentrated solution b cooled by heat exchange with the secondary refrigerant y in the thermal heat exchanger 5 is divided into a branch circuit 49, an absorption dilute solution pipe 48, a high temperature solution heat exchanger 7, an absorption dilute solution pipe 51, and a branch. It is supplied to the heating absorber 53 via the circuit 52, where it absorbs the water vapor a supplied from the gas-liquid separator 4 and becomes an absorption dilute solution c and is refluxed to the high-temperature regenerator 1. If it does in this way, conveyance of the primary refrigerant at the time of heating operation can be performed smoothly. Other effects areSecond reference exampleSince it is the same as in FIG.
【The invention's effect】
[0060]
  According to the first basic configuration of the present invention, the heat exchanger 5 for obtaining the heating heat source is connected to the primary refrigerant outlet side of the low temperature regenerator 6 during the cooling operation.And gas-liquid separator 4Therefore, the temperature of the thermal heat exchanger 5 is suppressed to the temperature of the saturated steam (about 100 ° C.), and abnormal overheating of the secondary refrigerant y in the thermal heat exchanger 5 is prevented, and 2 As a result of preventing decomposition of the fluorocarbon refrigerant used as the secondary refrigerant y, there is an excellent effect that the reliability of the apparatus can be ensured. Further, during the heating operation, the primary refrigerant vapor a (about 130 ° C.) is supplied from the gas-liquid separator 4 through the low-temperature regenerator 6 to the thermal heat exchanger 5. The heat possessed by the refrigerant vapor a is transmitted to the secondary refrigerant y as a heating heat source, and there is an effect that it is possible to prevent a decrease in the coefficient of performance (COP) during the heating operation.
[0061]
  In the first basic configuration of the present invention, the condensaterefluxWhen the circuit 21 is provided with the liquid seal portion 30 instead of the on-off valve 25, the on-off valve 25 can be omitted, which contributes to cost reduction.
[0062]
  According to the second basic configuration of the present invention, the thermal heat exchanger 5Heat exchangerIs disposed in the absorbent passage 6a in the low-temperature regenerator 6 so that the temperature of the thermal heat exchanger 5 can be suppressed to about 100 ° C. during the cooling operation. Therefore, the secondary refrigerant in the thermal heat exchanger 5 The abnormal overheating of y is prevented, the decomposition of the chlorofluorocarbon refrigerant used as the secondary refrigerant y is prevented, and there is an excellent effect that the reliability of the apparatus can be ensured. Further, during heating operation, the heat held by the absorbing liquid (about 130 ° C.) supplied from the gas-liquid separator 4 to the low-temperature regenerator 6 is transmitted to the secondary refrigerant y as a heating heat source. There is also an effect that it is possible to prevent a decrease in the coefficient of performance (COP) during the heating operation.
[0063]
  In the second basic configuration of the present invention, the intermediate concentrated solution b supplied from the gas-liquid separator 4 to the low-temperature regenerator 6 and the absorbed dilute solution refluxed from the air-cooled absorber 15 to the gas-liquid separator 4 a high-temperature solution heat exchanger 7 that exchanges heat with c, and a bypass circuit 32 that bypasses the high-temperature solution heat exchanger 7 and opens only during heating operation in the pipe 31 through which the intermediate concentrated solution b flows. In this case, the intermediate concentrated solution b that bypasses the high-temperature solution heat exchanger 7 (that is, heat is not recovered by the high-temperature solution heat exchanger 7 in the absorbed dilute solution c) is supplied to the low-temperature regenerator 6 during heating operation. Further, it is possible to prevent a decrease in the coefficient of performance (COP) during the heating operation while effectively performing the heat recovery to the absorbing dilute solution c refluxed to the high temperature regenerator 1 during the cooling operation.
[0064]
  According to the third basic configuration of the present invention, the intermediate concentrated solution b supplied from the gas-liquid separator 4 to the low-temperature regenerator 6 and the absorbing dilute solution c refluxed from the air-cooled absorber 15 to the gas-liquid separator 4. The heat heat exchanger 5 is disposed downstream of the high temperature solution heat exchanger 7 that exchanges heat with the heat exchanger 5 so that the temperature of the heat heat exchanger 5 is absorbed downstream of the high temperature solution heat exchanger 7 during cooling operation. Since the liquid temperature is suppressed to about 130 ° C., abnormal overheating of the secondary refrigerant y in the thermal heat exchanger 5 is prevented, and decomposition of the chlorofluorocarbon refrigerant used as the secondary refrigerant y is prevented. Thus, there is an excellent effect that the reliability of the apparatus can be ensured. Further, during the heating operation, the heat held by the intermediate concentrated solution b (about 130 ° C.) that has passed through the high-temperature solution heat exchanger 7 from the gas-liquid separator 4 is transmitted to the secondary refrigerant y as a heating heat source. Therefore, there is an effect that it is possible to prevent a decrease in the coefficient of performance (COP) during the heating operation.In addition, the absorption concentrated solution b supplied to the primary refrigerant passage of the thermal heat exchanger 5 during the heating operation enters the heating absorber 53, where it absorbs the primary refrigerant vapor a to become an absorption diluted solution c and has a high temperature. Since it is made to recirculate | reflux to the regenerator 1, there also exists an effect that conveyance of the primary refrigerant | coolant at the time of heating operation can be performed smoothly.
[0065]
  In the third basic configuration of the present invention, when the thermal heat exchanger 5 and the high-temperature solution heat exchanger 7 are integrated, the cost can be reduced.
[Brief description of the drawings]
FIG. 1 is a circuit diagram showing a refrigeration cycle of an air-cooled absorption refrigeration apparatus according to a first embodiment of the present invention.
FIG. 2 is a circuit diagram showing a refrigeration cycle of an air-cooled absorption refrigeration apparatus according to a second embodiment of the present invention.
FIG. 3 is a circuit diagram showing a refrigeration cycle of an air-cooled absorption refrigeration apparatus according to a third embodiment of the present invention.
FIG. 4 of the present inventionFirst reference exampleIt is a circuit diagram which shows the refrigerating cycle of the air cooling absorption refrigerating device concerning.
FIG. 5 of the present inventionSecond reference exampleIt is a circuit diagram which shows the refrigerating cycle of the air cooling absorption refrigerating device concerning.
FIG. 6 of the present inventionSecond reference exampleIt is the perspective view which saw through the inside of the heat exchanger unit in the air cooling absorption refrigeration apparatus concerning.
FIG. 7 of the present inventionThird reference exampleIt is a circuit diagram which shows the refrigerating cycle of the air cooling absorption refrigerating device concerning.
FIG. 8 shows the first aspect of the present invention.4It is a circuit diagram which shows the refrigerating cycle of the air cooling absorption refrigerating device concerning embodiment of this.
FIG. 9 shows the first aspect of the present invention.4It is the perspective view which saw through the inside of the heat exchanger unit in the air cooling absorption refrigerating device concerning this embodiment.
[Explanation of symbols]
  1 is a high-temperature regenerator, 4 is a gas-liquid separator, 5 is a thermal heat exchanger, 6 is a low-temperature regenerator, 6a is an absorbing liquid passage, 9 is an air-cooled condenser, 11 is a refrigerant pump, 12 is an evaporator, 15 is An air-cooled absorber, 17 is a use side heat exchanger, 18 is a solution pump, 21 is a condensate reflux circuit, 25 is an on-off valve, 30 is a liquid seal, 32 is a bypass circuit, 33 is an on-off valve, and 43 is a second Thermal heat exchanger, 53 is an absorber for heating, a is a primary refrigerant vapor (water vapor), b is an absorbing concentrated solution (lithium bromide concentrated solution), c is an absorbing diluted solution (lithium bromide diluted solution), d is Primary refrigerant condensate (condensed water), X is a primary refrigerant circuit, Y is a secondary refrigerant circuit, and y is a secondary refrigerant.

Claims

A primary refrigerant circulates, a high temperature regenerator (1), a gas-liquid separator (4), a heat heat exchanger (5) for obtaining a heating heat source, a low temperature regenerator (6), an air-cooled condenser (9), A primary refrigerant circuit (X) formed by sequentially connecting an evaporator (12) and an air-cooled absorber (15) for obtaining a cooling heat source, and a secondary refrigerant (y) circulate, and the thermal heat exchanger (5 ), An air-cooled absorption refrigeration apparatus comprising a use side heat exchanger (17) and a secondary refrigerant circuit (Y) formed by sequentially connecting the evaporator (12), wherein the secondary refrigerant (y) And a hot heat exchanger (5) is interposed between the primary refrigerant outlet of the low temperature regenerator (6) and the gas-liquid separator (4). the heat heat exchanger (5) and gas-liquid separator (4) returning condensate circuit and communicating (21), closed during the cooling operation, heating operation Air-cooled absorption type refrigerating apparatus being characterized in that interposed off valve to be opened (25) to.

The air-cooled absorption refrigeration apparatus according to claim 1, wherein the condensate reflux circuit (21) is provided with a liquid seal portion (30) instead of the on-off valve (25).

A primary refrigerant circulates, a high temperature regenerator (1), a gas-liquid separator (4), a heat heat exchanger (5) for obtaining a heating heat source, a low temperature regenerator (6), an air-cooled condenser (9), A primary refrigerant circuit (X) formed by sequentially connecting an evaporator (12) and an air-cooled absorber (15) for obtaining a cooling heat source, and a secondary refrigerant (y) circulate, and the thermal heat exchanger (5 ), An air-cooled absorption refrigeration apparatus comprising a use side heat exchanger (17) and a secondary refrigerant circuit (Y) formed by sequentially connecting the evaporator (12), wherein the secondary refrigerant (y) As a refrigerant, a heat exchange section of the thermal heat exchanger (5) to which the secondary refrigerant (y) is supplied is arranged in the absorption liquid passage (6a) in the low temperature regenerator (6). An air-cooled absorption refrigeration apparatus characterized by being provided.

An intermediate concentrated solution (b) supplied from the gas-liquid separator (4) to the low-temperature regenerator (6) and an absorbed dilute solution refluxed from the air-cooled absorber (15) to the gas-liquid separator (4) The high temperature solution heat exchanger (7) for exchanging heat with (c) and the pipe (31) through which the intermediate concentrated solution (b) flows bypass the high temperature solution heat exchanger (7) and perform heating operation. The air-cooled absorption refrigeration apparatus according to claim 3, further comprising a bypass circuit (32) that is opened only occasionally.

A primary refrigerant circulates, a high temperature regenerator (1), a gas-liquid separator (4), a heat heat exchanger (5) for obtaining a heating heat source, a low temperature regenerator (6), an air-cooled condenser (9), A primary refrigerant circuit (X) formed by sequentially connecting an evaporator (12) and an air-cooled absorber (15) for obtaining a cooling heat source, and a secondary refrigerant (y) circulate, and the thermal heat exchanger (5 ), An air-cooled absorption refrigeration apparatus comprising a use side heat exchanger (17) and a secondary refrigerant circuit (Y) formed by sequentially connecting the evaporator (12), wherein the secondary refrigerant (y) As an intermediate concentrated solution (b) supplied from the gas-liquid separator (4) to the low-temperature regenerator (6) and the air-cooled absorber (15) to the gas-liquid separator ( 4) A high-temperature solution heat exchanger (7) for exchanging heat with the diluted diluted solution (c) to be refluxed is attached and the high-temperature solution heat exchange is performed. The heat heat exchanger downstream of (7) (5) while disposing the primary of the outlet of the primary refrigerant passage in heat heat exchanger (5), from the gas-liquid separator (4) Heating absorber (53) which is supplied with refrigerant vapor (a) and is higher than the thermal heat exchanger (5) and at the same height as or lower than the gas-liquid separator (4) An air-cooled absorption refrigeration apparatus connected to the high-temperature regenerator (1) via

6. The air-cooled absorption refrigeration apparatus according to claim 5, wherein the thermal heat exchanger (5) and the high-temperature solution heat exchanger (7) are integrated.